EP0080098B1 - Verfahren zur Herstellung von 1,2-Dichlorethan - Google Patents

Verfahren zur Herstellung von 1,2-Dichlorethan Download PDF

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Publication number
EP0080098B1
EP0080098B1 EP82110276A EP82110276A EP0080098B1 EP 0080098 B1 EP0080098 B1 EP 0080098B1 EP 82110276 A EP82110276 A EP 82110276A EP 82110276 A EP82110276 A EP 82110276A EP 0080098 B1 EP0080098 B1 EP 0080098B1
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EP
European Patent Office
Prior art keywords
reaction
loop
zone
reaction zone
line
Prior art date
Legal status (The legal status is an assumption and is not a legal conclusion. Google has not performed a legal analysis and makes no representation as to the accuracy of the status listed.)
Expired
Application number
EP82110276A
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German (de)
English (en)
French (fr)
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EP0080098A1 (de
Inventor
Joachim Dr. Hundeck
Hans Hennen
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Hoechst AG
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Hoechst AG
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Publication date
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    • C—CHEMISTRY; METALLURGY
    • C07—ORGANIC CHEMISTRY
    • C07C—ACYCLIC OR CARBOCYCLIC COMPOUNDS
    • C07C17/00—Preparation of halogenated hydrocarbons
    • C07C17/013—Preparation of halogenated hydrocarbons by addition of halogens
    • C07C17/02—Preparation of halogenated hydrocarbons by addition of halogens to unsaturated hydrocarbons

Definitions

  • the invention relates to a process for the preparation of 1,2-dichloroethane by reacting ethylene and chlorine in liquid 1,2-dichloroethane in the presence of a catalyst customary for this, the heat of reaction generated in the reaction being used to advantage and the undesired formation of more chlorinated products such as tri, tetra and pentachloroethane, largely avoided in the reactor and the accumulation of such products in the reaction zone is prevented.
  • Chlorination of olefins using chlorine is known to be an exothermic reaction.
  • the exothermicity is 2200 kJ per kilogram of 1,2-dichloroethane.
  • the production of a ton of 1,2-dichloroethane thus generates a quantity of heat which is sufficient to generate about 1 ton of steam.
  • the heat of reaction was either removed by cooling the reactor or it was partly used for the direct evaporation and abortion of the dichloroethane formed in the reaction from the reaction mixture or the reactor and in some cases also for the exclusive rectification of after other procedure made 1,2-dichloroethane more or less fully used.
  • a combined removal of the heat of reaction in the chlorination of ethylene with chlorine is also practiced, for example, in the process described in DE-PS 1543108.
  • the iron reactor provided for carrying out the reaction is provided with a cooling device, to which cooling water is applied in order to dissipate heat generated during the reaction and to be able to maintain the reaction temperature of 50-70 ° C. predetermined for the reaction.
  • Compliance with the reaction temperature below the boiling point of 1,2-dichloroethane is regulated during the reaction in such a way that the 1,2-dichloroethane formed is continuously removed from the reaction space in the vapor state.
  • DE-OS 2935884 A method which corresponds in principle to the method of DE-PS 1543108 is disclosed in DE-OS 2935884, the characteristic features of the latter method being that the reactor charge is circulated during the reaction via a ring line connected to the reactor and the vaporous products withdrawing at the top of the reactor are separated in a rectification column to obtain 1,2-dichloroethane. Higher-boiling by-products are disadvantageously returned from the bottom of the rectification column to the reactor, so that in this case a separate work-up of discontinuously withdrawn amounts of reaction bottoms is required and the heat of reaction can only be partially used.
  • the recycling of the bottom product into the reactor is disadvantageous in that the circulating liquid medium is enriched with higher-boiling chlorination products, which have to be removed from the latter.
  • the proportion of 1,1,2-trichloroethane in the circulating medium is about 60%. This means that the known chlorination reaction proceeds with the formation of considerable proportions of undesirable by-products.
  • the invention now relates to a preferred embodiment of the process according to EP-AI-75.742, in that the process is carried out in a double-loop reactor.
  • inert gases or low-boiling hydrocarbons, such as ethyl chloride, contained in the reaction mixture are passed from the residence zone (5) via line (11) or from the descending part of the loop (I) via line (12 ) subtracts.
  • the circulation of the liquid medium in the reactor is effected according to the thermosiphon or mammoth pump principle.
  • the circulation speed of the liquid medium in the mixing zone should not be less than 0.1 m / sec.
  • the circulation to Product evaporation in the relaxation zone also takes place according to the thermosiphon principle.
  • the heat exchanger can be integrated into the product cycles or fed separately using a pump.
  • a double-loop reactor with loop circuits I and II is first charged with liquid 1,2-dichloroethane and the latter is circulated by introducing ethylene via line 1 and chlorine gas via line 2 according to the mammoth pump principle. After the reaction of the ethylene with the chlorine gas, which begins in the mixing zone 3 loaded with packing and is completed in the reaction zone 4 and in the dwell zone 5, an additional buoyancy arises in the ascending part of the loop I, due to the heat of reaction released.
  • the temperature in loop circuit 1 is somewhat lower than the boiling temperature of 1,2-dichloroethane at the pressure prevailing in the reactor.
  • any inert gases present in the loop are drawn off via lines 11 and 12 and cooled in a cooler (not shown in the drawing) for the condensation of 1,2-dichloroethane vapors carried along.
  • the uncondensed gases are blown off and worked up in a known manner.
  • the desired pressure can be set in the loop I by regulating the flow of inert gas with regard to the amount blown off.
  • two partial streams are branched off from the liquid stream, one partial stream for the delivery of thermal energy via the feed line 8 passing through the heat exchanger 10 and then returning via line 9 to the descending part of the loop I while the second partial flow of the loop II integrally connected to the loop I and a relaxation zone 6 located in the loop circuit II flows in, in which an adequate amount of the reaction product formed in the reaction zone 4 evaporates from the second partial flow, the vapors via the discharge line 7 in the Drawing, not shown, are supplied to the fractionation column, while the non-evaporated, liquid portion of the second partial stream returns via the descent part of the loop 11 into the mixing zone 3 or reaction zone 4 of the loop I.
  • Inert gases or low-boiling hydrocarbons, such as ethyl chloride, contained in the reaction mixture are withdrawn from the dwell zone 5 via line 11 or from the descending part of loop I via line 12.
  • the method of the invention is distinguished by the same advantages as are inherent in the method according to EP-A1-75.742. They result from the continuous removal of part of the liquid reactor contents and its division into two partial streams, of which one partial stream enables the continuous recovery of the heat of reaction, while the partial evaporation of the second partial stream and the exclusive working up of the steam portion in the fractionation column means that only catalyst-free Crude dichloroethane enters the fractionation column. With the above-mentioned vapors, however, the higher-chlorinated by-products are also fed to the fractionation column, thereby avoiding the accumulation of by-products in the loop circuit I.
  • the process sequence according to the invention also reduces the average residence time of all substances involved in the reaction under the given reaction conditions in the reactor to such an extent that undesirable side reactions leading to by-product formation are largely avoided.
  • the method of the invention also enables the use of starting products contaminated with inert gases, which are known to cause difficulties in the purification of the dichloroethane in the fractionation column.
  • these inert gases are already drawn off from the loop 1 via the inert gas lines 11 and 12, so that they cannot interfere with the further work-up process of the reaction mixture.
  • the method of the invention also proves to be advantageous over the method according to EP-A1-75.742 in that the use of a double-loop reactor, in which the continuous circulation of the reaction mixture in the loops and 11 takes place according to the thermosiphon or mammoth pump principle, the use of special pumps to promote the reaction mixture from or into the reactor is unnecessary, which is also associated with an energy saving.
  • Condensable components were separated in a cold trap at -30 ° C. from the reactor exhaust gas, which left the dwell zone 5 via line 11. Via line 7, 480.1 g / h of dichloroethane were drawn off in vapor form from the expansion vessel 6 and condensed.

Landscapes

  • Chemical & Material Sciences (AREA)
  • Organic Chemistry (AREA)
  • Organic Low-Molecular-Weight Compounds And Preparation Thereof (AREA)
  • Low-Molecular Organic Synthesis Reactions Using Catalysts (AREA)
  • Acyclic And Carbocyclic Compounds In Medicinal Compositions (AREA)
EP82110276A 1981-11-21 1982-11-08 Verfahren zur Herstellung von 1,2-Dichlorethan Expired EP0080098B1 (de)

Applications Claiming Priority (2)

Application Number Priority Date Filing Date Title
DE19813146246 DE3146246A1 (de) 1981-11-21 1981-11-21 Verfahren zur herstellung von 1,2-dichlorethan
DE3146246 1981-11-21

Publications (2)

Publication Number Publication Date
EP0080098A1 EP0080098A1 (de) 1983-06-01
EP0080098B1 true EP0080098B1 (de) 1984-09-12

Family

ID=6146933

Family Applications (1)

Application Number Title Priority Date Filing Date
EP82110276A Expired EP0080098B1 (de) 1981-11-21 1982-11-08 Verfahren zur Herstellung von 1,2-Dichlorethan

Country Status (14)

Country Link
EP (1) EP0080098B1 (enrdf_load_stackoverflow)
JP (1) JPS5892626A (enrdf_load_stackoverflow)
AR (1) AR231831A1 (enrdf_load_stackoverflow)
AU (1) AU564581B2 (enrdf_load_stackoverflow)
BR (1) BR8206726A (enrdf_load_stackoverflow)
CA (1) CA1221708A (enrdf_load_stackoverflow)
DD (1) DD206775A5 (enrdf_load_stackoverflow)
DE (2) DE3146246A1 (enrdf_load_stackoverflow)
ES (1) ES517343A0 (enrdf_load_stackoverflow)
HU (1) HU191194B (enrdf_load_stackoverflow)
MX (1) MX161860A (enrdf_load_stackoverflow)
NO (1) NO155575C (enrdf_load_stackoverflow)
SU (1) SU1480758A3 (enrdf_load_stackoverflow)
ZA (1) ZA828536B (enrdf_load_stackoverflow)

Families Citing this family (12)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
DE3340624C1 (de) * 1983-11-10 1984-10-11 Dynamit Nobel Ag, 5210 Troisdorf Verfahren zur Herstellung von 1,2-Dichlorethan aus Ethylen und Chlorgas
DE3445896C1 (de) * 1984-12-15 1986-04-10 Dynamit Nobel Ag, 5210 Troisdorf Verfahren zur kontinuierlichen Herstellung von 1.2-Dichlorethan
JPH0723327B2 (ja) * 1985-12-09 1995-03-15 三井東圧化学株式会社 １，２−ジクロルエタン生成熱の回収法
DE4026282A1 (de) * 1990-08-20 1992-02-27 Hoechst Ag Verfahren und vorrichtung zur herstellung von hochreinem 1,2-dichlorethan mit waermerueckgewinnung
DE4318609A1 (de) * 1993-01-27 1994-07-28 Hoechst Ag Verfahren und Vorrichtung zur Herstellung von 1,2-Dichlorethan durch Direktchlorierung
DE19910964A1 (de) * 1999-03-12 2000-09-21 Krupp Uhde Gmbh Verfahren zur Herstellung von Ethylendichlorid (EDC)
RU2162834C1 (ru) * 2000-03-15 2001-02-10 Общество с ограниченной ответственностью "ИНИС" Способ получения 1,2-дихлорэтана
RU2004102204A (ru) 2001-06-28 2005-06-10 Сумитомо Кемикал Компани, Лимитед (Jp) Способ очистки хлора и способ получения 1,2-дихлорэтана
FR2878171B1 (fr) * 2004-11-19 2007-03-09 Solvay Reacteur et procede pour la reaction entre au moins deux gaz en presence d'une phase liquide
DE102004063090A1 (de) * 2004-12-22 2006-07-06 Uhde Gmbh Verfahren zur Herstellung von 1,2-Dichlorethan mittels Direktchlorierung
DE102005044177A1 (de) * 2005-09-15 2007-04-05 Uhde Gmbh Verfahren und Vorrichtung zur Nutzung der bei der Reinigung von 1,2-Dichlorethan anfallenden Kondensationswärme
CN103360203B (zh) * 2013-07-03 2014-07-09 中国海洋石油总公司 一种综合利用炼化干气并生产二氯乙烷的方法

Family Cites Families (4)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
BE725636A (enrdf_load_stackoverflow) * 1968-12-18 1969-06-18
GB1422303A (en) * 1973-06-11 1976-01-28 Stauffer Chemical Co Production of ethylene dichloride
DE2743975B1 (de) * 1977-09-30 1979-03-01 Bayer Ag Verfahren zur Herstellung eines praktisch Vinylchlorid-freien 1,2-Dichloraethans
DE2935884A1 (de) * 1979-09-05 1981-04-02 Wacker-Chemie GmbH, 8000 München Verfahren zur herstellung von 1.2-dichlorethan

Also Published As

Publication number Publication date
DE3260738D1 (en) 1984-10-18
DD206775A5 (de) 1984-02-08
EP0080098A1 (de) 1983-06-01
HU191194B (en) 1987-01-28
ES8307692A1 (es) 1983-08-01
BR8206726A (pt) 1983-10-04
DE3146246A1 (de) 1983-05-26
SU1480758A3 (ru) 1989-05-15
AU564581B2 (en) 1987-08-20
NO823884L (no) 1983-05-24
ZA828536B (en) 1983-10-26
JPS5892626A (ja) 1983-06-02
NO155575C (no) 1987-04-22
JPH0235729B2 (enrdf_load_stackoverflow) 1990-08-13
NO155575B (no) 1987-01-12
AU9074982A (en) 1983-05-26
CA1221708A (en) 1987-05-12
MX161860A (es) 1991-01-30
AR231831A1 (es) 1985-03-29
ES517343A0 (es) 1983-08-01

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